EP2107302A1 - Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée - Google Patents

Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée Download PDF

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Publication number
EP2107302A1
EP2107302A1 EP08305077A EP08305077A EP2107302A1 EP 2107302 A1 EP2107302 A1 EP 2107302A1 EP 08305077 A EP08305077 A EP 08305077A EP 08305077 A EP08305077 A EP 08305077A EP 2107302 A1 EP2107302 A1 EP 2107302A1
Authority
EP
European Patent Office
Prior art keywords
oxide
average particle
reactor
particle diameter
separation device
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP08305077A
Other languages
German (de)
English (en)
Other versions
EP2107302B1 (fr
Inventor
Laurent Maghdissian
Jean-Claude Semedard
Pierre Gauville
Corinne Beal
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
General Electric Technology GmbH
Original Assignee
Alstom Technology AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to EP08305077.3A priority Critical patent/EP2107302B1/fr
Application filed by Alstom Technology AG filed Critical Alstom Technology AG
Priority to ES08305077.3T priority patent/ES2483723T3/es
Priority to PCT/EP2009/053096 priority patent/WO2009121713A1/fr
Priority to AU2009231348A priority patent/AU2009231348B2/en
Priority to CA2718075A priority patent/CA2718075C/fr
Priority to US12/935,315 priority patent/US20110023760A1/en
Priority to CN200980111770.0A priority patent/CN101981376B/zh
Publication of EP2107302A1 publication Critical patent/EP2107302A1/fr
Application granted granted Critical
Publication of EP2107302B1 publication Critical patent/EP2107302B1/fr
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/002—Fluidised bed combustion apparatus for pulverulent solid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/033—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment comminuting or crushing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/99008—Unmixed combustion, i.e. without direct mixing of oxygen gas and fuel, but using the oxygen from a metal oxide, e.g. FeO
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/80—Shredding
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/503—Fluidised bed furnace with two or more fluidised beds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a process for using a facility for burning carbonaceous solid materials and relating facility, in order to produce electricity and/or steam.
  • the solid materials can be fossil fuels such as coal, for example, waste or biomass, and they are injected into a combustion chamber, for example a fluidized bed combustion chamber.
  • Such a facility for burning carbonaceous materials is described in patent document FR 2 850 156 .
  • This facility includes a reactor for reducing oxides, a first cyclone, a reactor for oxidizing oxides, a second cyclone, exchangers for controlling temperature of the circulating oxides and exchangers for flue gas heat recovery.
  • the facility circulate oxides which are reduced and then oxidized in the two reactors.
  • the solid fuel material is grounded before entering the oxide reduction reactor, and in the case of coal the average particle diameter is less than 500 ⁇ m.
  • the oxides are reduced by having them in contact with the fuel which reacts with the oxygen released by the oxides and then oxidized by contact with air which regenerates the oxides.
  • the oxides have a particle size range from 50 to 500 ⁇ m and a density from 2000 to 7000 kg/m 3 .
  • the average diameter of particles of entering coal is about 300 ⁇ m in conventional fluidized bed combustion chambers. This leads to circulating particle diameter of about 150 ⁇ m.
  • This type of facility for combustion of carbonaceous solid materials operating at atmospheric pressure with integrated capture of carbon dioxide does not require any prior air separation. Because of the simplicity and the compactness of this system, the costs of capturing carbon dioxide may be reduced while providing production of steam for generating electricity.
  • the solid particles at the outlet of the first cyclone associated with the reduction reactor consisting of oxides particles and of carbonaceous residues, pass through a seal pot and are then directed towards a device for removing the carbonaceous residues.
  • This removal device is fluidized by steam. With this fluidization, the fine and light particles such as the carbonaceous residues may be separated and re-introduced into the reduction reactor, while the denser and larger oxide particles are transferred towards the oxidation reactor.
  • This removal device which is a separator contains an internal baffle formed with a wall integral with the roof of the separator and leaving a flow space in the bottom of the latter and which forms two compartments on the passage of fluidized solids with a pressure seal provided by the height of the fluidized solids, between the two compartments.
  • the fluidization of each compartment is independently controlled by two steam inlets, in order to obtain the desired velocity field for separating the oxides and the carbonaceous residues in the first compartment as well as the transfer of the oxides into the second compartment. Above the first compartment, a vent brings the carbonaceous residues carried off by steam back towards the reduction reactor.
  • This separator is a carbon barrier in the facility, essential for capturing carbon dioxide which is a greenhouse gas which should be subject to emission restrictions.
  • the object of patent document WO 2007/113016 is to increase the yield of this barrier by improving such a separator.
  • the segregation phenomenon is enhanced, while increasing the time for treating the solid materials in the first compartment and keeping a separator of limited size.
  • the object of the invention is to improve such facility in order that an easier separation of carbonaceous residues and oxides is obtained, and in order to assure that no carbonaceous residues will be sent to the reactor for oxidizing oxides. This is obtained by using non conventional coal particle size in order to lead to a lower efficiency requirement on the carbon separator and then to achieve the carbon dioxide capture.
  • the invention relates to a process for using a facility in which circulates at least one oxide which is reduced and then oxidized in each of both reactors and including a first reactor for reducing oxide in which enter a grounded solid fuel material and oxide, a first separation device receiving entrained solids from this reactor for reducing oxide, a carbon separator installed at the outlet of this first separation device in order to send the carbonaceous particles into the reactor for reducing oxide and the oxide into a second reactor for oxidizing oxide and a second separation device receiving entrained solids from this reactor for oxidizing oxide, process characterized in that the average particle diameter of the entering solid fuel material is controlled to be different from the average particle diameter of the entering oxide, with a rate of relating average particle diameters of at least two.
  • Solid fuel material is preferably coal.
  • Said oxide can be metal oxide. It can be limestone too.
  • the metal oxide can be based on iron, nickel, alumina or a mixture thereof.
  • the average particle diameter of the entering solid fuel material is greater than the average particle diameter of the entering oxide.
  • the average particle diameter of the entering solid fuel material is preferably equal to about 500 ⁇ m.
  • the average particle diameter of the entering solid fuel material is smaller than the average particle diameter of the entering oxide.
  • the reduced size of the solid fuel particles allows more complete and faster combustion.
  • the reactor for reducing oxide can be consequently of smaller size.
  • the average particle diameter of the entering solid fuel material is equal to about 50 ⁇ m.
  • the invention relates too to a facility for implementing the process according to the second embodiment, characterized in that the said first separation device is a low efficiency cyclone and that it comprises other separation device connected to the finest particles outlet of this first separation device.
  • the said first separation device has such efficiency that the average particle diameter of the finest particles fraction escaping from this first separation device is about equal to said average particle diameter of the entering solid fuel material.
  • the other separation device is a separation cyclone.
  • the said first separation device is a separation cyclone. It can be a mechanical separator by impact too.
  • the facility can comprise a solid cooling device implemented in between the first separation device and the said other separation cyclone.
  • the figure 1 is a schematic view of a facility according to a first embodiment of the invention.
  • the figure 2 is a schematic view of a facility according to a second embodiment of the invention.
  • a facility for combusting carbonaceous solid materials, in order to produce electricity and/or steam, according to the invention, in which circulates at least one oxide, preferably a mixture of oxides, advantageously metal oxides, which is reduced and then oxidized includes a first reactor 1 for reducing oxides in which enter a grounded solid fuel material E1 and oxides E2 , a first separation cyclone 2 feeding with entrained solids from this reactor for reducing oxides, a carbon separator 3 installed at the outlet of this first cyclone in order to send the carbonaceous particles into the reactor for reducing oxides 1 and the oxides into a second reactor 4 for oxidizing oxides fluidized by air 13 and a second separation cyclone 5 feeding with entrained solids from the reactor for oxidizing oxides.
  • a first reactor 1 for reducing oxides in which enter a grounded solid fuel material E1 and oxides E2
  • a first separation cyclone 2 feeding with entrained solids from this reactor for reducing oxides
  • the facility comprises two back pass 11, 12, containing recovery exchangers for the flue gases and for the air, each dedicated to one of the reactors.
  • the average particle diameter of the entering solid fuel material E1 is equal to about 50 ⁇ m and the solid fuel material is preferably coal.
  • the reactor 1 for reducing oxides is fluidized by a mixture A1 of steam and recycled flue gas. After reduction in the reactor 1 for reducing oxides, the oxides enter the first cyclone 2 in which the solid oxides particles are separated from the carbonaceous residues and the combustion gases, consisting of CO2, SO2 and steam.
  • the first separation cyclone 2 is a low efficiency cyclone and the facility comprises other separation apparatus 6 of high efficiency connected at the upper outlet of this first cyclone 2 and which is preferably a separation cyclone too.
  • the first separation cyclone 2 has such efficiency that the average particle diameter of the upper stream escaping from this first separation cyclone is about equal to said average particle diameter of the entering solid fuel material E1 i.e. equal to about 50 ⁇ m.
  • a solid cooling device 10 is implemented in between the first separation cyclone 2 and the other separation cyclone 6.
  • fly ash and the combustion gases then enter the heat exchangers contained into back pass 11, downstream cyclones 2 and 6.
  • the seal pot can be fluidized by steam and/or recycled flue gas.
  • the separator 3 is fluidized by steam and/or recycled flue gas, which separates out the fine and light particles, such as the carbon-containing residue, which is fed to the first reactor 1 for reducing oxides, while the denser and larger oxides particles are fed to the second reactor 4 for oxidation.
  • the solid separator 3 is of the type of separator described in patent document WO 2007/113016 .
  • the oxides and the depleted air enter the cyclone 5, in which the solid oxides particles are separated from the gases, consisting essentially of N2 and 02.
  • the solid oxides particles extracted from the bottom of the second cyclone 5 enter a seal pot 9 from which a first portion is transferred to the bottom of the second reactor 4 for oxidizing oxides, a second portion is recirculated to the bottom of the first reactor 1 for reducing oxides and a third portion is sent to an external bed 7 fluidized by air where heat exchangers are implemented, and finally fed to the second reactor 4 for oxidizing oxides.
  • the seal pot can be fluidized with compressed air. The complete cycle of the various reactions is described next.
  • the solid grounded fuel E1 is injected into the first reactor 1 for reducing oxides, which contains a circulating bed of oxides at a high temperature of 700°C to 1 150°C. According to the invention, it is preferably grounded coal with an average particle diameter equal to about 50 ⁇ m.
  • the particle size range of the fuel avoids the accumulation of coarse ash at the bottom of the first reactor 1 for reducing oxides, that has to be extracted, and produces almost 100% fly ash. Therefore ash does not accumulate in the circulating bed of coarser oxides, which is collected by the first cyclone 2.
  • Metal oxides E2 are injected into the first reactor 1 for reducing oxides too. According to the invention, it is preferably metal oxides with an average particle diameter equal to or greater than 100 ⁇ m.
  • the volatile materials are released very quickly following heating of the fuel and react with the oxygen given off by the oxides to achieve partial combustion that continues with the combustion of the fixed carbon.
  • the solids are circulated after in the first separation cyclone 2 which has such efficiency that the average particle diameter of the solids escaping from this first separation cyclone is about equal 50 ⁇ m. These solids are mainly composed of carbonaceous residues.
  • This upper fraction of the solids which is constituted by carbon, is circulated into the other separation cyclone 6 installed in series with the first one 2, in order to separate the solids from the gases and to re-introduce the carbonaceous materials into the first reactor 1 for reducing oxides.
  • a first separation of the carbonaceous residues from the metal oxides is obtained by means of the series of the first cyclone 2 of low efficiency and the other separation cyclone 6.
  • the lower fraction of solids at the outlet of first cyclone 2 is extracted at the bottom of the seal pot 8 to be cleaned of the carbon-containing residues in the solid separator 3, and is then fed to the second reactor 4 for oxidizing oxides in order to be oxidized by the oxygen in the air atmosphere.
  • the oxides enter the second reactor 4 for oxidizing oxides, and regenerated after entering the second reactor 4 for oxidizing oxides are partly fed to the first reactor 1 for reducing oxides to start a new cycle of transport of oxygen from the second reactor 4 for oxidizing oxides to the first reactor 1 for reducing oxides.
  • the quantity of oxides fed to the first reactor 1 for reducing oxides is controlled by a solids flow rate control valve (not shown).
  • the device can also be pressurized.
  • the oxygen depleted air is cooled in exchangers and de-dusted by a bag filter before it is discharged to the atmosphere.
  • a facility for combusting carbonaceous solid materials, in order to produce electricity and/or steam, according to the invention, in which circulates at least one oxide, preferably a mixture of oxides, advantageously metal oxides, which is reduced and then oxidized includes a first reactor 1 for reducing oxides in which enter a grounded solid fuel material E1 and oxides E2 , a first separation cyclone 20 feeding with entrained solids from this reactor for reducing oxides, a carbon separator 3 installed at the outlet of this first cyclone in order to send the carbonaceous particles into the reactor for reducing oxides 1 and the oxides into a second reactor 4 for oxidizing oxides fluidized by air 13 and a second separation cyclone 5 feeding with entrained solids from the reactor for oxidizing oxides.
  • a first reactor 1 for reducing oxides in which enter a grounded solid fuel material E1 and oxides E2
  • a first separation cyclone 20 feeding with entrained solids from this reactor for reducing oxides
  • the facility comprises two back pass 11, 12, containing recovery exchangers for the flue gases and for the air, each dedicated to one of the reactors.
  • This facility is of the type of the known facility described in patent document FR 2 850 156 .
  • the solid grounded fuel E1 is injected into the first reactor 1 for reducing oxides, which contains a circulating bed of oxides at a high temperature. According to the invention, it is preferably grounded coal with an average particle diameter equal to about 500 ⁇ m.
  • the particle size range of the fuel assures the accumulation of solid fuel at the bottom of the first reactor 1 for reducing oxides and its greater residence time in this reactor 1 and the solids leaving the reactor are essentially constituted by oxides, which is collected in the conventional first cyclone 20.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Cyclones (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Combined Means For Separation Of Solids (AREA)
EP08305077.3A 2008-04-01 2008-04-01 Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée Not-in-force EP2107302B1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
ES08305077.3T ES2483723T3 (es) 2008-04-01 2008-04-01 Procedimiento para usar una instalación para quemar materiales carbonosos e instalación relacionada
EP08305077.3A EP2107302B1 (fr) 2008-04-01 2008-04-01 Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée
AU2009231348A AU2009231348B2 (en) 2008-04-01 2009-03-16 Process for using a facility for combusting carbonaceous materials and relating facility
CA2718075A CA2718075C (fr) 2008-04-01 2009-03-16 Procede d'utilisation d'une installation pour la combustion de materiaux carbones et installation associee
PCT/EP2009/053096 WO2009121713A1 (fr) 2008-04-01 2009-03-16 Procédé d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée
US12/935,315 US20110023760A1 (en) 2008-04-01 2009-03-16 Process for using a facility for combusting carbonaceous materials and relating facility
CN200980111770.0A CN101981376B (zh) 2008-04-01 2009-03-16 使用用于燃烧含碳物料的设备的方法及相关设备

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP08305077.3A EP2107302B1 (fr) 2008-04-01 2008-04-01 Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée

Publications (2)

Publication Number Publication Date
EP2107302A1 true EP2107302A1 (fr) 2009-10-07
EP2107302B1 EP2107302B1 (fr) 2014-05-14

Family

ID=39940609

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08305077.3A Not-in-force EP2107302B1 (fr) 2008-04-01 2008-04-01 Processus d'utilisation d'une installation pour la combustion de matériaux carbonés et installation associée

Country Status (7)

Country Link
US (1) US20110023760A1 (fr)
EP (1) EP2107302B1 (fr)
CN (1) CN101981376B (fr)
AU (1) AU2009231348B2 (fr)
CA (1) CA2718075C (fr)
ES (1) ES2483723T3 (fr)
WO (1) WO2009121713A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011066376A2 (fr) 2009-11-30 2011-06-03 Chevron U.S.A. Inc. Procédé et système destinés à capturer du dioxyde de carbone dans un procédé de combustion en boucle dans lequel l'oxygène est fourni par des sorbants oxydes métalliques pouvant être régénérés
FR2960940A1 (fr) * 2010-06-02 2011-12-09 Inst Francais Du Petrole Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2960941B1 (fr) * 2010-06-02 2014-11-14 Inst Francais Du Petrole Dispositif de separation de particules pour une boucle de combustion chimique
WO2013115884A2 (fr) 2011-11-15 2013-08-08 Trustees Of Boston University Inhibiteurs de virus, de type pyridopyrimidinone
CN103486576A (zh) * 2013-09-25 2014-01-01 上海锅炉厂有限公司 一种三反应器结构的化学链燃烧装置和方法
CN107255282A (zh) * 2017-05-05 2017-10-17 浙江新都绿色能源有限公司 一种垃圾焚烧过程中飞灰的循环利用工艺
US11142717B2 (en) * 2019-03-22 2021-10-12 General Electric Company Hybrid boiler-dryer and method

Citations (4)

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Publication number Priority date Publication date Assignee Title
FR2850156A1 (fr) 2003-01-16 2004-07-23 Alstom Switzerland Ltd Installation de combustion avec recuperation de co2
FR2895413A1 (fr) * 2005-12-27 2007-06-29 Alstom Technology Ltd Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone
WO2007104655A1 (fr) * 2006-03-16 2007-09-20 Alstom Technology Ltd Installation pour produire de l'electricite
WO2007113016A1 (fr) 2006-02-02 2007-10-11 Alstom Technology Ltd. Séparateur de solides en particulier pour équipement de combustion

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US4400181A (en) * 1982-01-28 1983-08-23 Hydrocarbon Research, Inc. Method for using fast fluidized bed dry bottom coal gasification
US4572085A (en) * 1985-02-06 1986-02-25 Amax Inc. Coal combustion to produce clean low-sulfur exhaust gas
US4823712A (en) * 1985-12-18 1989-04-25 Wormser Engineering, Inc. Multifuel bubbling bed fluidized bed combustor system
FI873735A0 (fi) * 1987-08-28 1987-08-28 Ahlstroem Oy Foerfarande och anordning foer foergasning av fast kolhaltigt material.

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2850156A1 (fr) 2003-01-16 2004-07-23 Alstom Switzerland Ltd Installation de combustion avec recuperation de co2
FR2895413A1 (fr) * 2005-12-27 2007-06-29 Alstom Technology Ltd Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone
WO2007113016A1 (fr) 2006-02-02 2007-10-11 Alstom Technology Ltd. Séparateur de solides en particulier pour équipement de combustion
WO2007104655A1 (fr) * 2006-03-16 2007-09-20 Alstom Technology Ltd Installation pour produire de l'electricite

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011066376A2 (fr) 2009-11-30 2011-06-03 Chevron U.S.A. Inc. Procédé et système destinés à capturer du dioxyde de carbone dans un procédé de combustion en boucle dans lequel l'oxygène est fourni par des sorbants oxydes métalliques pouvant être régénérés
EP2506954A2 (fr) * 2009-11-30 2012-10-10 Chevron U.S.A. Inc. Procédé et système destinés à capturer du dioxyde de carbone dans un procédé de combustion en boucle dans lequel l'oxygène est fourni par des sorbants oxydes métalliques pouvant être régénérés
EP2506954A4 (fr) * 2009-11-30 2014-12-24 Chevron Usa Inc Procédé et système destinés à capturer du dioxyde de carbone dans un procédé de combustion en boucle dans lequel l'oxygène est fourni par des sorbants oxydes métalliques pouvant être régénérés
AU2010324744B2 (en) * 2009-11-30 2015-10-01 Chevron U.S.A. Inc. Method and system for capturing carbon dioxide in an oxyfiring process where oxygen is supplied by regenerable metal oxide sorbents
FR2960940A1 (fr) * 2010-06-02 2011-12-09 Inst Francais Du Petrole Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede
WO2011151535A3 (fr) * 2010-06-02 2012-01-19 IFP Energies Nouvelles Procede de combustion en boucle chimique avec une zone de reaction integrant une zone de separation gaz-solide et installation utilisant un tel procede
US9927118B2 (en) 2010-06-02 2018-03-27 Total Sa Chemical looping combustion method with a reaction zone including a gas-solid separation zone and plant using same

Also Published As

Publication number Publication date
CA2718075C (fr) 2016-05-10
EP2107302B1 (fr) 2014-05-14
US20110023760A1 (en) 2011-02-03
CN101981376A (zh) 2011-02-23
AU2009231348A1 (en) 2009-10-08
CN101981376B (zh) 2016-05-11
AU2009231348B2 (en) 2013-05-30
CA2718075A1 (fr) 2009-10-08
WO2009121713A1 (fr) 2009-10-08
ES2483723T3 (es) 2014-08-07

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